Influence of Nickel on Biomass Pyro-Gasification - ACS Publications

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Influence of nickel on biomass pyro-gasification: coupled thermodynamic and experimental investigations Marwa Said, Laurent Cassayre, Jean-Louis Dirion, Ange Nzihou, and Xavier Joulia Ind. Eng. Chem. Res., Just Accepted Manuscript • DOI: 10.1021/acs.iecr.7b05201 • Publication Date (Web): 26 Feb 2018 Downloaded from http://pubs.acs.org on February 26, 2018

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Industrial & Engineering Chemistry Research

Influence of nickel on biomass pyro-gasification: coupled thermodynamic and experimental investigations Marwa Said (1),(2) · Laurent Cassayre(2),* · Jean‑Louis Dirion (1) · Ange Nzihou (1) Xavier Joulia (2)

(1)

Université de Toulouse, Mines Albi, CNRS, Centre RAPSODEE, Campus Jarlard, F-81013 Albi cedex 09, France Laboratoire de Génie Chimique, Université de Toulouse, CNRS, INPT, UPS, 4, Allée Emile Monso, F-31030 Toulouse, France

(2)

* Corresponding author. E-mail address: [email protected]

Abstract The present research falls within the scope of the chemical influence of heavy metals on thermochemical conversion of biomass. Specifically, the impact of nickel during pyrolysis and CO2-gasification of willow samples was studied by experimental and thermodynamic approaches. For this purpose, willow wood samples were impregnated with various contents of nickel. The pyro-gasification tests were performed in a laboratory fixed bed reactor, providing the chemical composition of solid residue and major gases. Our thermodynamic simulations, based on a specific calculation procedure, were found to corroborate most of the experimental data. In addition to these methodological findings, the main results of the study are: (i) Ni has a noticeable catalytic activity even at low contents (between 0.016 and 0.086 mol per kg of wood) (ii) due to the low oxygen potential of the system C + CO2, Ni stays in an active metal form as long as some carbon is left in the reactor (iii) Ni prevents the volatilization of sulfur during the gasification, due to the formation of a stable Ni3S2 solid phase.

Keywords:

pyro-gasification;

contaminated

biomass;

nickel;

catalytic

effect;

thermodynamics.

ACS Paragon Plus Environment

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1. Introduction Biomass is considered to be the only natural and renewable carbon resource that can effectively substitute fossil fuels. Additionally, it is especially abundant and stands as the third energy resource after oil and coal1. Among the many options for biomass processing, several thermochemical conversion processes are appealing, such as combustion for heat and electricity production, and pyro-gasification with the addition of a gasification agent such as H2O or CO2. Moreover, biomass gasification in the presence of CO2 would offer a potential solution for the alleviation of greenhouse gas emission.

Wastes, such as contaminated biomass, constitute widely available resources for these conversion processes. Plants used for phytoextraction represent an accessible resource of such contaminated biomass. These plants are used to extract contaminants from polluted soils, and heavy metals (HM) accumulate inside the roots, stems and leaves2. For example, the concentration of zinc in crops grown on contaminated soils can reach 4 g/kg in contaminated willow leaves3, and up to 10 g/kg of nickel in the tissues of some hyperaccumulators4. Houzelot et al.5 even studied specific plants allowing nickel content as high as 150 g/kg. Waste biomass such as demolition wood, chromated copper arsenate timber, de-inking sludge, sewage sludge or spent pot liner constitute many other examples of contaminated biomass that can contain high amounts of HM.

Currently, contaminated biomass is hardly used in thermochemical conversion processes, due to its potentially high content in HM. Given the large quantities of these resources, many studies investigate the behavior and the effect of the HM during their thermochemical conversion. It has been shown that HM distribute unevenly between ash, gases and tars. Their behavior mainly depends on their initial content in the biomass, and on their chemical form during the thermal conversion2,3. The HM vaporization, and more generally the inorganic elements behavior, has been widely studied not only with the aim of reducing the emissions of toxic elements in the environment during industrial combustion processes6,7, but also in order to manage related technical issues (agglomeration of fluidized beds, slag formation, deposition and corrosion phenomena on heat exchangers)8,9. A body of work has also shown that some HM have a significant influence on reaction kinetics. Depending on their nature, these HM have a catalytic or inhibitory effect on


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thermochemical conversion reactions10. As a consequence, finely divided particles of nickel, cobalt or iron11 are sometimes used as catalysts in thermochemical conversion processes.

In order to improve the understanding of HM behavior and/or influence during thermochemical conversion of biomass, two main methods (sometimes combined) are usually applied. The first method consists in carrying out measurements and analysis of pyro-gasification products in laboratory or industrial installations. The TGAs (ThermoGravimetric Analyzers) are usually used to identify the kinetics of the gasification reaction12,13. The fixed-bed reactor is widely used thanks to its ease of operation. Other studies are carried out in fluidized bed reactors, which is a widely developed industrial gasification technology14. For example, Syc et al.14 studied the behavior of Cd, Cu, Ni, Pb and Zn during steam gasification of a mixture of oak and beech wood in a fluidized bed reactor. They showed that cadmium is the most volatile metal and that it is mainly present in the gas phase, while nickel is found in the ashes. The authors concluded that the vaporization of the heavy metals decreases as follows: Cd >> Pb> Zn> Cu> Ni. Collard et al.15, Bru et al.16 and Richardson et al.17 inserted intentionally by impregnation, some HM (Ni, Cu and Fe ) into the biomass in order to improve the contact between the catalyst and the biomass and optimize the conversion efficiency. Other researchers18,19 investigated the reactivity of various biomass chars, in the presence of different metals, in CO2 atmosphere using different kinetic models to fit with the reactivity data. They found that the gasification reactivity of metal-containing chars was higher than that of the chars obtained from raw biomass.

The second approach relies on the investigation of thermodynamic calculations, which may be a valuable computational approach to predict and understand the behavior of elements during thermal treatment of biomass and waste. In some recent studies20–23, specific calculations procedure were developed, in order to take into account the highly non-equilibrium behavior of organic matter during thermal treatment and its influence on inorganics’ behavior.

In the present research, we focus on understanding the impact of the nickel content on the thermal decomposition of a biomass heated in a CO2 atmosphere. The methodology combines experimental measurements (in a thermogravimetric device and a fixed bed


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reactor) and thermodynamic simulations. The main research questions concern (i) the determination of the chemical form of nickel during the main steps of the thermal treatment (pyrolysis up to 450°C, gasification up to 950°C), (ii) the influence of nickel on the main conversion reactions and (iii) on the behavior of other inorganic elements. The selected biomass is willow, which exhibit high HM absorption capacity. Since natural contaminated biomass is very heterogeneous and usually contains many metals whose roles can interfere24, the willow samples were prepared by impregnation of various Ni contents. Based on our previous study25, we chose impregnation conditions adapted to the understanding of the effect of Ni without modifying the wood structure. In the following sections, our experimental data are discussed in the light of a thermodynamic approach that we developed in previous research (databases aspects26, calculation procedure aspects27).

2. Materials and methods 2.1. Experimental procedure 2.1.1. Samples preparation The willow wood pellets, supplied by ‘pépinières-Naudet’ company (France), were dried, crushed and sieved to a range of particle size of 0.5 - 1 mm. About 30 g of willow wood particles were then impregnated in 300 mL of nickel nitrate aqueous solutions, prepared with 3 different amounts of Ni(NO3)2·6H2O (Sigma–Aldrich, 99 % purity). The obtained mixtures were stirred at ambient temperature for 24 hours. According to our previous study25, the Ni concentration in the aqueous solution had to be below 0.1 mass %, in order to avoid significant modifications of the wood structure and noticeable washing of some elements (mostly Ca, K and S). Therefore, the selected solution concentrations were 0.01, 0.05 and 0.07 mass % of Ni respectively. The resulting Ni concentration in the impregnated wood samples, were validated by elemental analysis (see section 2.1.3) and correspond to 0.09, 0.34 and 0.48 wt %, respectively. The Ni concentrations are close to those usually found in the literature for phytoextraction plants, where the Ni contents are usually comprised between 0.1 to 1 wt %28,29. In the following, the samples are labeled “wood-X-Ni”, X being the Ni concentration (in wt %) in the wood samples. “Raw-wood” corresponds to a non-impregnated wood.


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2.1.2. Pyro-gasification devices Thermal treatments were carried out using two devices: a fixed-bed reactor, with 5 g of wood, and a thermo-gravimetric analyzer (TGA), with 15 mg of wood. The reactor is composed of a quartz tube, in which the wood samples are held by a sintered porous quartz disk (see our previous work25 for more details). The wood samples are first heated at 5 °C/min, under N2 flow (6 L/h), up to 450 °C. After 1 hour at 450 °C, a mixed atmosphere (5.4 L/h of CO2 and 0.6 L/h of N2) is flushed in the reactor, and the furnace is heated at 5 °C/min, from 450 to 950 °C. The sample is then kept for one hour at 950 °C, before cooling. An additional experiment was carried out with wood-0.34-Ni and stopped when the temperature reached 800 °C. These operating conditions were selected in order to complete the sample pyrolysis before the start of the gasification. Even if there is some interference between the thermal degradation step and the gasification step, this protocol is the best compromise in order to illustrate the influence of Ni content on both type of reactions, and for the two reactors. Solid residues are collected after treatment at 450 °C (henceforth char) and at 950 °C (henceforth ash). All solid samples are weighed and characterized. The gases are collected in successive 0.5 L sampling bags, and analyzed by a gas chromatograph equipped with two analytical columns. This protocol provides the quantitative amount of major gases N2, O2, H2, CO, CH4, CO2, C2H4 and C2H6. The thermogravimetric measurements are carried using a TGA/DTA analyzer (SDT Q600) under atmospheric pressure. About 15 mg of sample is placed in a platinum crucible. The analyses are performed in the same conditions (temperature and atmosphere) as in the pyro-gasification reactor. Each TGA is repeated three times and the mean standard deviation of weight loss is lower than 1 %. Due to the low initial amount of wood, the solid residues are not characterized. 2.1.3. Sample analyses The CHN contents of the different samples (raw wood, impregnated wood, char and ash) are determined with an elemental analyzer (Flash 2000). The ash content of each sample is measured according to the standard FN-EN-ISO-18122, which consists in an air oxidation at 550 °C. The oxygen content is determined by mass balance. For the determination of inorganics, the samples are mineralized with a specific mineralization protocol and analyzed on Inductively Coupled Plasma Optical Emission


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Spectroscopy (ICP-OES). For wood and char, 200 mg samples are immersed in 2 mL of oxygenated water and 8 mL of nitric acid. The mixture is placed in a special fluoroplastic flask (PTFE), which is inserted in a pressure digestion vessel made of high alloy stainless steel SS 316 Ti (DAB-2). The vessel is heated in an electric heating block for 4 hours at 200 °C under high pressure (max 200 bar). For ashes, 40 mg samples are attacked by a mixture of hydrogen peroxide and nitric acid and then heated for 10 hours at 200 °C under the same conditions as those described for char. Each measurement is repeated three times. The samples compositions are provided in Table 1, in mol per kg of wood (mol.kgw-1). For all elements (except Ni), the reported composition is the mean value measured in the four wood samples (Raw wood, Wood-X-Ni with X = 0.09, 0.34 and 0.48). The precision indicated in Table 1 corresponds thus to the standard deviation of twelve measurements (three analyses of each four samples).

Table 1. Elemental composition of wood samples. Element H C O N Ca F K S Si Ni content (mol.kgw-1)

mol.kgw-1 59.70 ± 3.1 ˟ 10-1 41.23 ± 1.3 ˟ 10-1 27.67 ± 1.1 ˟ 10-1 0.51 ± 5.0 ˟ 10-2 1.03 ˟ 10-1 ± 1.9 ˟ 10-3 7.18 ˟ 10-2 ± 3.4 ˟ 10-2 1.96 ˟ 10-2 ± 1.4 ˟ 10-3 1.84 ˟ 10-2 ± 2.7 ˟ 10-3 1.25 ˟ 10-2 ± 2.6 ˟ 10-3 Raw wood 4.44 ˟ 10-4

mol.kgw-1 Element mol.kgw-1 -2 1.22 ˟ 10 3.32 ˟ 10-4 P Sn -3 ± 1.4 ˟ 10 ± 1.7 ˟ 10-5 -3 7.92 ˟ 10 2.66 ˟ 10-4 Mg Mn -3 ± 2.0 ˟ 10 ± 3.9 ˟ 10-5 -3 6.03 ˟ 10 2.25 ˟ 10-4 Na Pb ± 9.3 ˟ 10-4 ± 2.7 ˟ 10-5 2.97 ˟ 10-3 1.81 ˟ 10-4 Al Sb -4 ± 4.3 ˟ 10 ± 6.3 ˟ 10-5 -3 2.36 ˟10 1.65 ˟ 10-4 Cl Cd -3 ± 1.2 ˟ 10 ± 1.1 ˟ 10-5 -3 1.45 ˟ 10 1.36 ˟ 10-4 Fe Cr -4 ± 2.7 ˟ 10 ± 2.0 ˟ 10-5 -4 7.56 ˟ 10 6.93 ˟ 10-5 Zn Co ± 1.5 ˟ 10-4 ± 6.3 ˟ 10-6 4.54 ˟ 10-4 3.49 ˟ 10-5 B Ba -5 ± 9.0 ˟ 10 ± 5.7 ˟ 10-6 -4 4.38 ˟ 10 Cu ± 7.4 ˟ 10-5 Wood-0.09-Ni Wood-0.34-Ni Wood-0.48-Ni 1.61 ˟ 10-2 5.74 ˟ 10-2 8.45 ˟ 10-2

Element

All solid residues are also characterized by X-Ray diffraction, with a Philips PANalytical X’Pert MPD diffractometer using Cu (Kα) radiation. Data acquisition is performed between 10 and 70° in 2θ with a step of 0.017° (2θ).


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2.2. Thermodynamic calculation methodology In our previous work27, a specific calculation methodology was selected out of several options by comparing equilibrium calculations with the elemental composition (27 elements listed in Table 1) of raw willow wood ashes after CO2 pyro-gasification. The main features of the selected procedure are presented in this section. 2.2.1. Software and database Equilibrium calculations are performed with FactSage 7.030. In order to describe the complex system composed of 27 elements, a specific selection of the compounds available within the FactSage package led to the final choice of 373 gaseous, 247 liquid and 1115 solid species. Within this selection, there are 10 gaseous, 10 liquid and 66 solid Ni-containing compounds. Two liquid solution phases were also selected: (i) SALTF, which describes liquid salts solutions (Na, K//F, Cl, CO3) with low melting points (ii) SLAGA, which describes liquid silicates solutions (Si, K, Ca // O, S) with high melting points31. 2.2.2. Calculations conditions The calculations are performed on 1 kg of wood. The input composition, for which Ni is the only variable, is provided in Table 1. The fixed conditions for the calculations are the pressure (1 bar) and the nature of the gasification agent (CO2). The procedure consists in calculating the equilibrium every 10 °C, from 450 °C to 950 °C. At each calculation step, a constant amount of CO2 (in mol.kgw-1) is added in the system, and the equilibrium composition is recorded. After each computation step, the gas phase is removed from the system in order to simulate an open system in which the gaseous species are not in contact with the condensed phases (Figure 1). Five additional steps are computed at 950 °C, in order to simulate the temperature plateau.

Figure 1. Principle of open system equilibrium calculations.


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2.2.3. Determination of During CO2 gasification of char, the main reaction is the oxidation of carbon according to the so-called Boudouard reaction: C(s) + CO2(g) = 2 CO(g) When C(s) has fully reacted, the exhaust gas is thus mainly composed of unreacted CO2(g). As illustrated in Figure 2, the amount of CO2 which is added in the system at each calculation step () plays an important role on the temperature at which total carbon cunsumption occurs. Carbon cunsumption temperature / °C

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Tstep=20°C

950

Tstep=10°C Tstep=5°C

850

750

650 0

2

4

6

8

10

12

14

/ mol.kg-1 Figure 2. Evolution of the temperature of full carbon conversion with the amount of CO2 added at each calculation step.

In our simulations, is adjusted so that the total consumption of carbon occurs at the same temperature as in the experimental reactor. Adjusting is thus a simple way of introducing a kinetic restriction on the main gasification reaction. It can be noted from Fig. 2 that if the temperature step is different from 10°C, the value will be modified proportionally: is divided by 2 for a temperature step of 5°C, and multiplied by 2 for a temperature step of 20°C. This is consistent with the Boudouard equilibrium, since the carbon consumption at a given temperature is only depending on the CO2 partial pressure. The measured variation of CO(g) and CO2(g) concentration in the exhaust gases is plotted in Figure 3. The total conversion of carbon occurs when the temperature reaches 950 °C. was thus set to 1.25 mol.kgw-1 (see Fig. 2), which is smaller than the experimental amount of CO2 (1.78 mol.kgw-1) flushed through the reactor during the 2 min necessary


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to raise the temperature by 10 °C, indicating that, on average, about 30 % of the CO2 does not take part in the gasification reaction. It can be noted that for another reactor or operating conditions, the same methodology could be applied. would then be obtained from experimental measurements of CO2 and CO concentration profiles in the exhaust gases. These data are easy to obtain for any reactor with standard chromatography techniques.

1.0

molar fraction in gas phase

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CO2(g)-exp. 0.8

CO2(g)-calc.

0.6

= 1.25 0.4 CO(g)-calc. 0.2 CO(g)-exp. 0.0 450

550

650

750

850

950

950

Temperature / °C

Figure 3. Comparison of the temperature evolution of CO2 and CO molar fraction in the gas phase (i) measured in fixed bed reactor with raw wood (symbols and dashed lines) and (ii) calculated with = 1.25 mol.kgw-1 (continues lines).

The discrepancy between calculated and measured gas composition is large (temperature shift up to 200 °C), and is the direct consequence of kinetics control of gasification reactions. However, the main tendency (i.e. a large increase of CO proportion, followed by a significant drop after total carbon consumption) is represented with such calculation procedure, using one single parameter, which is not the case with closed system calculations27.

3. Results and discussion 3.1. Catalytic effect of Ni

3.1.1. Thermogravimetric analyses Figure 4 shows the thermal analyses of the wood samples, which is divided into three main zones: the first temperature increase from 30 to 450°C (A), the plateau at 450°C for 1 hour (B) and the second temperature raise to 950°C, with a CO2 flush (C). The pyrolysis


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step (A and B) was carried out under N2, and the gasification step (C) under 90 % CO2 and 10 % of N2. raw-wood wood-0.34-Ni

wood-0.09-Ni wood-0.48-Ni Temperature

100 % N2

1000

90 % CO2 + 10 % N2

80

800

60

600

C

B

A 40

400

20

200

0

Temperature / °C

100

TG / %

1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60

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0 0

30

60

90

120 150 180 Time / min

210

240

270

300

Figure 4. TG profiles of willow wood samples during pyro-gasification.

In Zone A, after a slight mass loss at about 100 °C corresponding to the water evaporation, a major mass loss occurs between 200 and 450 °C. As already finely described in the literature, this step corresponds to the hemicellulose and cellulose pyrolysis32. In Zone B, the mass loss at the end of the isotherm increases by 6 % for the wood-0.34Ni and by 8 % for the wood-0.48-Ni samples compared to raw wood. This feature is a clear indication of the influence of Ni on the pyrolysis step. The gasification step (zone C) starts with the input of CO2 at t = 144 min. The differential of the TG signal (DTG) is presented in Figure 5 for zone C. For the impregnated samples wood-0.34-Ni and wood-0.48-Ni, an additional reaction is evidenced in the temperature range 470-660 °C. The DTG signal is more intense at high Ni concentrations. Furthermore, the main gasification reaction, which reaches a maximum rate at around 910 °C on raw wood, is shifted to lower temperatures with increasing amount of impregnated Ni (respectively 880 °C, 845 °C and 820 °C for wood-0.09-Ni, wood-0.34Ni and wood-0.48-Ni). Figure 5 also shows that the increase of the Ni content in the samples enhances the gasification rate and, as a consequence, the variation of the gasification reaction kinetics. These results are in-line with previous findings dealing with CO2 gasification kinetics. Indeed, Figueiredo et al.33 showed that the reactivity of impregnated carbon increases with the amount of Ni catalyst, with a decrease of the activation energy from 260 kJ.mol-


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1

without Ni to about 110 J.mol-1 for the Ni-catalyzed gasification reaction. Many other

studies led to the conclusion that the kinetic parameters of the gas-solid reactions during CO2 gasification are deeply affected by the presence and the amount of inorganic elements (either alkaline / alkaline-earth metals34 or transition metals19,33). Di Blasi35 stated that the char reactivity depends on three main characteristics: its porosity, its chemical structure and the quantity of inorganic constituents. As evidenced in previous studies17,34, all those characteristics change when the wood or the char contain a high amount of a metal element.

0.2

raw-wood wood-0.34-Ni dTG / mg.min-1

1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60


wood-0.09-Ni wood-0.48-Ni

0.15

0.1

0.05

0 460

560

660 760 Temperature / °C

860

Figure 5. DTG profiles of willow wood samples during gasification. Inlet gas flow is composed of 5.4 L/h of CO2 + 0.6 L/h of N2.

The effect of Ni on the pyrolysis and gasification products is further discussed in the following sections based on the data collected with the fixed-bed reactor. 3.1.2. Fixed bed reactor experiments analysis The same experimental protocol (described in section 2.1.b) for the TG analysis is used for the bed reactor experiments. •

Pyrolysis step in fixed bed reactor

The mass balance of the pyrolysis products, taking account gases, char and tars, is presented in Table 1. Around 18-20 % of the initial mass is missing. This is attributed to the condensation of tars on the reactor walls and in the gas circuit. Tars recovery is indeed a major and recurrent experimental difficulty, which requires the development of specific devices that were not available in our configuration. Nevertheless, the impact of Ni is


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rather clear from our experimental data: it leads to an increase of the total amount of gas and a decrease of the final amount of char. Table 2. Mass balance of the products obtained from the willow wood samples pyrolysis in a fixedbed reactor where T ranges from ambient to 450 °C in inlet gas flow of 6 L/h (N2).

gas yield / wt %

char yield / wt %

tar yield / wt %

total / wt %

raw-wood

14.1 ± 0.4

30.4 ± 0.4

36.6 ± 2.1

81.1 ± 2.9

Wood-0.09-Ni

14.5 ± 0.6

29.7 ± 0.6

37.9 ± 1.4

82.1 ± 2.6

Wood-0.34-Ni

15.0 ± 0.2

29.6 ± 0.9

36.2 ± 2.4

80.8 ± 3.5

Wood-0.48-Ni

17.2 ± 0.1

28.9 ± 1.0

34.0 ± 2.6

80.1 ± 3.7

The organic elemental composition and the ash content of the four samples of chars produced at 450 °C-60 min are presented in Table S1. The data show that both carbon and hydrogen contents in the chars decrease with the rise of the Ni content, in favor of the ash content. The highest variation is observed for hydrogen, with a decrease of 30 % in the wood-0.48-Ni sample compared to the raw-char. This variation of the elemental composition of the chars agrees well with the amount and composition of gases produced during pyrolysis. The comparison of the impact of Ni impregnation on the total amount of H2 and CO (in moles of gas formed per kg of wood) is presented in Figure 6. Additional data concerning CO2, CH4, C2H4 and C2H6 yields are plotted in Figure S1. The gas composition analysis shows a strong increase of the H2 yield (multiplied by 6 and 14 times for wood-0.09-Ni and wood-0.48-Ni, respectively) and, to a lesser extent, of the CO formation (about 5 % for the wood-0.48-Ni sample).


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1.6

CO CO yield / mol.kg w-1

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1.5

1.4

1.3

1.2 0

0.02 0.04 0.06 Ni content / mol.kg w-1

0.08

0.1

Figure 6. Influence of Ni content on the total production of H2 and CO during pyrolysis of willow wood samples in a fixed-bed reactor where T ranges from ambient to 450 °C using an inlet gas flow of 6 L/h (N2).

Given all these results, we can conclude that Ni impregnation in willow wood leads to significant changes during the pyrolysis step: (i) an increase of the total amount of gas produced and of the H2 content in this gas, and (ii) a drop of the char amount and of the H content in this char. These phenomena are explained by a catalytic effect of Ni on biomass pyrolysis reactions (and more specifically on tars cracking inside the wood), as already well documented in the literature. For instance, Bru et al.16 and Collard et al.15 studied respectively the influence of Ni on the pyrolysis reactions of beech wood at 700 °C and oak wood at 600 °C. They both found a significant decrease in tar production in favor of gases, which is consistent with our results. Furthermore, Richardson et al.17 showed that nickel metal nanoparticles act as a catalytic active phase for enhancing H2 production during biomass pyrolysis. They also demonstrate that Ni is an active catalyst exclusively in its metal form related to a reduction reaction occurring between 450 and 600 °C. In these studies, Ni concentrations were ranging from 0.07 to 0.65 mol.kgw-1 and pyrolysis temperatures from 600 to 700 °C. In our study, we show that the catalytic effect of Ni on pyrolysis reactions is effective at lower temperature (450 °C) with Ni contents as low as 0.016 mol.kgw-1. •

Gasification in fixed bed reactor

Due to the low amounts of tars and ashes, as well as the difficulty to recover them, the mass balance of the gasification part of the experiment (ramp 450-950 °C + isotherm at 950 °C with CO2 flush) was not established.


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The total production of H2 and CO is presented in Figure 7. The nickel content has no significant impact on the overall CO yield. However, the catalytic effect of Ni is noticeable on the H2 yield with an increase of 1 % and 22 % for the wood-0.09-Ni and wood-0.48-Ni samples respectively. 1.6

30

1.4

28

CO yeild / mol.kg w-1

H 2 yield / mol.kg w-1

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1.2

1.0

H2 0.02

0.04

24 22

CO

0.8 0

26

0.06

0.08

0.1

20 0

Ni content / mol.kg w-1

0.02

0.04

0.06

0.08

0.1

Ni content / mol.kg w-1

Figure 7. Influence of Ni content on the total production of H2 and CO during gasification of willow wood samples in a fixed-bed reactor where T range from 450 to 950 °C while the inlet gas flow is 5.4 L/h of CO2 + 0.6 L/h of N2.

It is well attested that the CO2 gasification of char leads to the formation of CO by the Boudouard reaction and results in low values of H2/CO ratio36. In the present study, the H2/CO ratio is around 0.05, with a content of CO2 in the gas injected into the reactor equal to 88 %. This is rather consistent with the data compiled by Butterman et al.37, which mention a H2/CO ratio in the range of 0.1 to 1.0 for CO2 contents varying from 30 to 50% in the inlet gas, and a clear decrease of this ratio with increasing CO2 content. Furthermore, the increase of the Ni content in the sample rises the H2/CO value by 23 % compared to raw wood.

The production profiles of H2 and CO as a function of the temperature presented in Figure 8 provide more insights into the influence of the Ni content. Data for CH4 are provided in Figure S2. Significant changes related to Ni are evidenced on these profiles, essentially between 500 and 800 °C. The H2 yield increases by 55 to 118 % at 600 °C for wood-0.34-Ni and wood-048-Ni compared to raw wood, and H2 production stops at lower temperature in the presence of Ni. Similarly, the CO yield increase up to 1 mol.kgw-1 and 1.5 mol.kgw-1at 600 °C for wood-0.34-Ni and wood-0.48-Ni sample respectively, while it is negligible at low Ni content. The CO production reaches a maximum at 900 °C for the wood-0.34-Ni sample and at 800 °C for the wood-0.48-Ni sample. For the wood-0.09-


14

Page 15 of 26

Ni and raw wood, the maximum of CO production is detected at 900 °C and 950 °C respectively.

raw wood wood-0.34-Ni

wood-0.09-Ni wood-0.48-Ni

H2 0.15

0.10

CO yield / mol.kg w-1

0.20 H2 yield / mol.kg w-1

1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60


4

raw wood

wood-0.09-Ni

wood-0.34-Ni

wood-0.48-Ni

CO 3

2

0.05

1

0.00

0

Temperature / °C

Temperature / °C

Figure 8. Influence of temperature on the amount of H2 and CO produced during gasification of willow wood samples in a fixed-bed reactor using an inlet gas flow of 5.4 L/h CO2 + 0.6 L/h N2 25.

Combined with TGA analysis, the data collected from the fixed-bed reactor experiments provide a rather clear picture of the catalytic influence of Ni on gasification. Indeed, for Ni contents higher than 0.09 mol.kgw-1, an additional reaction occurs between 500 and 600 °C. This reaction results in a significant mass loss of the char, and produces noticeable amounts of H2(g) and CO(g). Furthermore, the presence of nickel in the samples decreases the temperature onset of the main gasification reaction, from 920 °C in raw wood down to 830 °C with wood-0.48-Ni.

The catalytic effect of nickel on both pyrolysis and gasification is thus clearly evidenced and characterized by quantification of the major reaction products (char, tars, H2, CO) during the process. Furthermore, this catalytic effect depends on the initial quantity of nickel. 3.2. Ni speciation 3.2.1. Speciation by XRD characterizations The XRD (x-ray diffraction) analyses of the char samples obtained by pyrolysis at 450 °C are presented in Figure 9. The diffraction patterns of the four samples show the presence of a dominant amorphous phase. The presence of graphite carbon, calcium carbonate and potassium carbonate is detected in all samples. A crystalline phase


15


corresponding to Ni metal (with fcc structure) is also evidenced in wood-0.34-Ni and wood-0.48-Ni samples, but it is not detectable in the wood-0.09-Ni sample. Furthermore, the diffractogram of the residue obtained at 800 °C also show the presence of nickel in its metal form (Figure 10).

1E+5

1E+5 C CaCO3 K2CO3 Ni

8E+4 Wood-0.48-Ni

6E+4 Wood-0.34-Ni

4E+4 wood-0.09-Ni

9E+4

*

8E+4

Intensity / counts

1E+5

Intensity / Coups

1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60

Page 16 of 26

Ni K2CO3 CaO

7E+4 Char - 450 °C

6E+4 5E+4 4E+4 3E+4

Char - 800 °C 2E+4

2E+4 raw-wood

20

30

40 2 Theta / °

50

60

Figure 9. XRD analyses of the char samples produced at 450 °C-60 min.

*

*

1E+4

0E+0 10

*

70

0E+0 10

20

30

40

50

60

70

2 Theta / °

Figure 10. XRD analyses of the chars produced at 450 °C-60 min and 800 °C for the wood0.34-Ni sample.

The X-ray diffractograms of the ashes recovered at the end of the pyro-gasification reaction are presented in Figure 11. They indicate the presence of nickel oxide (NiO) in the three impregnated samples, which shows that Ni metal undergoes oxidation at some point during the process.

Figure 11. XRD analyses of the ashes samples produced at 950 °C-60 min.

3.2.2. Speciation by thermodynamic calculations The calculated temperature evolution of the chemical speciation of nickel for three samples is presented in Figure 12. The Ni speciation results for the wood-0.48-Ni sample


16

Page 17 of 26

are similar to those found for the wood-0.34-Ni sample. For this reason, the speciation results of the wood-0.48-Ni sample are not included in Fig. 12. A first comment is that, independently of its initial quantity, Ni fully remains in condensed phases, either in solids or in the slag solution phase. In any case, Ni forms intermetallic compounds with Sb (NiSb) and Sn (Ni3Snx, with 1≤x≤3), which are the most stable compounds that bind to Ni among the 26 elements considered in the biomass. A consequence is that, for raw wood (for which Sb and Sn content is higher than the Ni content), there is no free Ni metal on the entire temperature range. When more Ni is available in the system (wood-0.09-Ni), a second type of compound forms (Ni3S2), which is stable up to about 700 °C. With higher Ni contents (wood-0.34-Ni and wood-0.48-Ni), Ni is predominantly present in its metal form through the whole temperature range.

8E-4

raw-wood 950°C

mol.kg-1

6E-4 Ni (SLAG A)

4E-4 2E-4

NiO

NiSb

Ni3Sn

Ni3Sn4

0E+0 450

550

0.03

Ni3Sn2

650 750 850 Temperature / °C

950

wood-0.09-Ni 950°C

mol.kg-1

1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60


0.02

Ni (SLAG A) NiSb + Ni 3Snx

0.01

NiO

Ni

Ni3S2 0.00 450

550



950

17


0.10

wood-0.34-Ni 950°C

mol.kg-1

0.08 Ni (SLAG A)

0.06 0.04

Ni3S2

NiO

Ni

0.02 0.00 450

550


950

Figure 12. Calculated Ni speciation as function of Ni content, for T=450 to 950 °C. Additional calculation steps for T=950 °C are represented on the right extremity of the x-axis.

At the end of the pyro-gasification reaction, when all carbon is consumed, nickel progressively oxidizes into NiO, as illustrated in Figure 12. According to the model, part of the oxide dissolves in the liquid slag phase. Figure 13 gives an additional insight into the behavior of Ni in the pyro-gasification reactor. Indeed, in the 450-950 °C temperature range, the equilibrium oxygen partial pressure (PO2) resulting of the equilibrium between CO2 and wood is lower than the equilibrium PO2 between Ni and NiO. This means that the stable form of nickel is the metal form. However, when all carbon has been consumed, the atmosphere switches to pure CO2(g), with a higher oxygen potential that leads to oxidation of Ni into NiO. 1.E-06

950°C

1.E-10

PO2 / atm

1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60

Page 18 of 26

1.E-14 1.E-18 1.E-22 1.E-26 1.E-30 450

550

650

750

850

950

Temperature / °C

Figure 13. Influence of temperature on oxygen partial pressure (PO2) at equilibrium: (i) Ni-NiO equilibrium (ii) raw wood.

3.2.3. Discussion The combination of XRD characterization and thermodynamic calculations provides a concordant picture on the behavior of Ni during the pyro-gasification. Indeed, nickel is detected in its metal form in solid residues recovered at 450 and 800 °C, provided that Ni


18

Page 19 of 26 1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60


quantity is sufficient for detection. The final ashes contain predominantly nickel oxide, due to its oxidation at the end of the process. As already mentioned, Ni must be in its metal form to cause a catalytic effect on the pyrogasification reactions. The thermodynamic speciation indicates that, at low temperature, sulfur has a high affinity with Ni. As reported in several experimental studies carried out on various Ni-based catalysts32,33, sulfur can be an important inhibitor of its catalytic activity. Therefore, a threshold content of Ni is required in the biomass to observe the catalytic effect of Ni. Below this threshold value, Ni is trapped in sulfide compounds. Furthermore, it is expected that at temperature higher than 700 °C, the decomposition of nickel sulfide enhances the catalytic effect of Ni.

3.3. Ni effect on the behavior of inorganic elements 3.3.1. Influence of Ni on ashes composition The elemental composition of ashes (measured and calculated with FactSage) is presented in Figure 14. The chemical analyses performed by ICP-OES indicate that the ashes are mainly composed of Ca, K, Mg, P, S and Si, plus a growing proportion of Ni for impregnated samples. This is consistent with the major phases identified by XRD (Figure 12): Ca5(PO4)3(OH), K2SO4, Ca3Mg(SiO4)2 and CaO, plus NiO. The calculated elemental composition of the ashes, determined as the sum of all solid compounds at 950 °C, reproduces remarkably well the experimental data. Apart from S, which behavior will be further discussed in the next section, both calculated and measured data show that there is no major influence of the initial Ni amount on the content of the main elements of the ashes.


19


Raw wood

Wood-0.09-Ni

Experimental

S Mn

Wood-0.34-Ni

Si

S

Wood-0.48-Ni

other

other

other Si

S

P

Si

Si

P

Ni

Mg

Ca

K

Ca

Ca

Ca

Mn

Ni

Ni

Mg

K

K

K Mg

Ni Mg

S P

S

Si

Si

other

S

S

Mg

other

Ca

Ca

Ca

Si

P

Ni

Ca

Mn

Si other

P

P

K

other

S

P

P

other

Calculated

1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60

Page 20 of 26

Ni

Ni

Mg K

K Mg

K

Mg

Figure 14. Comparison between experimental and calculated ashes elemental composition.

As discussed in our previous work27, the adopted calculation procedure leads to a satisfactory reproduction of trace elements contents measured in raw wood ashes recovered after CO2 gasification. The wood samples impregnated with Ni studied in the present work did not lead to major changes in the behavior of trace elements either. Some of them were shown to fully or partially volatilize: S, Cd, Pb, Zn, Cl, Sn, K, Na and F. 1.1.a. Influence of Ni on sulfur behavior As discussed in details by Kaknics et al.38, sulfur has been shown to volatilize to a large extent during pyro-gasification at low temperature, in the form of H2S(g) and COS(g), when placed in the reducing environment constituted by C(s) and CO2(g). Our experimental data confirm that, for raw wood, more than 50% of the initial sulfur is not found in the final solid residue. Furthermore, the amount of sulfur in the ashes increases significantly with the Ni content. These results are consistent with the calculated amount of S in gas phase presented in Figure 15. Indeed, Ni promotes the trapping of sulfur in a Ni3S2 solid phase up to about 650 °C. At higher temperature, S is then trapped in a CaS solid phase. When the initial nickel content is significantly higher than the sulfur content, most of sulfur is thus trapped in the solid residue. This behavior is rather similar to the observations from Mortensen39 and Woolcock40 in the case of nickel catalysts for methane reforming. The authors observed sulfur trapping on nickel, resulting in the catalyst’s poisoning.


20

Page 21 of 26

1.0 raw wood

Proportion of S in gas phase

1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60


0.8

0.6

wood-0.09-Ni

0.4

0.2

Ni3S2(s)

CaS(s)

wood-0.34-Ni & wood-0.48-Ni

0.0 450

550

650

750

850

950

Temperature (°C)

Figure 15. Calculated influence of temperature and Ni content on the proportion of sulfur in the gaseous phase.

4. Conclusions The combination of experimental and thermodynamic approaches helped to evaluate the role and the behavior of Ni during the pyro-gasification reaction of impregnated willow samples in CO2 atmosphere. The experimental tests allowed to quantify the solid and gaseous products during pyro-gasification. The thermodynamic simulation methodology consisted in (i) considering an open system to simulate a gas flow in the system (ii) determining the amount of gasification agent added at each calculation step with experimental measurements of CO2 and CO concentration profiles, these data being easy to obtain for any reactor with standard chromatography techniques. The thermodynamic simulations were consistent with most of the experimental data (chemical analysis of ashes, XRD of the solid residues at 450, 800 and 950 °C), even if the exact amount of Ni linked with a catalytic activity could not be determined with accuracy. Based on this methodological approach, the main results of the study are: •

Ni has a noticeable catalytic activity even at low contents (between 0.016 and 0.086 mol.kgw-1).

•

Ni stays in an active metal form as long as some carbon is left in the reactor due to the low oxygen potential of the system C + CO2,

•

Ni prevents the evaporation of sulfur during the gasification, due to the formation of a stable Ni3S2(s) phase.


21


Page 22 of 26

Our methodological contribution constitute a powerful approach that would allow for future investigation of the influence of other metals such as Cu and Fe during pyrogasification reactions, as well as detecting potential synergies between inorganic elements such as the Ni-S interactions evidenced in this work .

Supporting Information The Supporting Information is available free of charge on the ACS Publications website. List of content: Table S1 (Elementary composition of the chars); Figure S1 (Influence of Ni content on the total production of CnHm and CO2 during pyrolysis); Figure S2 (Influence of temperature on the amount of CH4 produced during gasification).

References (1)

Radmanesh, R.; Courbariaux, Y.; Chaouki, J.; Guy, C. A Unified Lumped Approach in Kinetic Modeling of Biomass Pyrolysis. Fuel 2006, 85, 1211–1220.

(2)

Gupta, A. K.; Sinha, S. Phytoextraction Capacity of the Plants Growing on Tannery Sludge Dumping Sites. Bioresour. Technol. 2007, 98, 1788–1794.

(3)

Lievens, C.; Carleer, R.; Cornelissen, T.; Yperman, J. Fast Pyrolysis of Heavy Metal Contaminated Willow: Influence of the Plant Part. Fuel 2009, 88, 1417– 1425.

(4)

Zhang, X.; Laubie, B.; Houzelot, V.; Plasari, E.; Echevarria, G.; Simonnot, M.-O. Increasing Purity of Ammonium Nickel Sulfate Hexahydrate and Production Sustainability in a Nickel Phytomining Process. Chem. Eng. Res. Des. 2015, 106, 26–32.

(5)

Houzelot, V.; Laubie, B.; Pontvianne, S.; Simonnot, M.-O. Effect of up-Scaling on the Quality of Ashes Obtained from Hyperaccumulator Biomass to Recover Ni by Agromining. Chem. Eng. Res. Des. 2017, 120, 26–33.

(6)

Wu, S.; Xu, Y.; Sun, J.; Cao, Z.; Zhou, J.; Pan, Y.; Qian, G. Inhibiting Evaporation of Heavy Metal by Controlling Its Chemical Speciation in MSWI Fly Ash. Fuel 2015, 158, 764–769.

(7)

Toledo, J. M.; Corella, J.; Corella, L. M. The Partitioning of Heavy Metals in Incineration of Sludges and Waste in a Bubbling Fluidized Bed. 2. Interpretation of Results with a Conceptual Model. J. Hazard. Mater. 2005, 126, 158–168.


22

Page 23 of 26 1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60


(8)

Šyc, M.; Pohořelý, M.; Jeremiáš, M.; Vosecký, M.; Kameníková, P.; Skoblia, S.; Svoboda, K.; Punčochář, M. Behavior of Heavy Metals in Steam Fluidized Bed Gasification of Contaminated Biomass. Energy Fuels 2011, 25, 2284–2291.

(9)

Yuan, C.-S.; Lin, H.-Y.; Wu, C.-H.; Liu, M.-H. Partition and Size Distribution of Heavy Metals in the Flue Gas from Municipal Solid Waste Incinerators in Taiwan. Chemosphere 2005, 59, 135–145.

(10)

Nzihou, A.; Stanmore, B. The Fate of Heavy Metals during Combustion and Gasification of Contaminated Biomass-a Brief Review. J. Hazard. Mater. 2013, 256–257, 56–66.

(11)

Sutton, D.; Kelleher, B.; Ross, J. R. H. Review of Literature on Catalysts for Biomass Gasification. Fuel Process. Technol. 2001, 73, 155–173.

(12)

Lahijani, P.; Zainal, Z. A.; Mohamed, A. R.; Mohammadi, M. CO2 Gasification Reactivity of Biomass Char: Catalytic Influence of Alkali, Alkaline Earth and Transition Metal Salts. Bioresour. Technol. 2013, 144, 288–295.

(13)

Huo, W.; Zhou, Z.; Chen, X.; Dai, Z.; Yu, G. Study on CO2 Gasification Reactivity and Physical Characteristics of Biomass, Petroleum Coke and Coal Chars. Bioresour. Technol. 2014, 159, 143–149.

(14)

Šyc, M.; Pohořelý, M.; Kameníková, P.; Habart, J.; Svoboda, K.; Punčochář, M. Willow Trees from Heavy Metals Phytoextraction as Energy Crops. Biomass Bioenergy 2012, 37, 106–113.

(15)

Collard, F.-X.; Blin, J.; Bensakhria, A.; Valette, J. Influence of Impregnated Metal on the Pyrolysis Conversion of Biomass Constituents. J. Anal. Appl. Pyrolysis 2012, 95, 213–226.

(16)

Bru, K.; Blin, J.; Julbe, A.; Volle, G. Pyrolysis of Metal Impregnated Biomass : An Innovative Catalytic Way to Produce Gas Fuel. J. Anal. Appl. Pyrolysis 2007, 78, 291–300.

(17)

Richardson, Y.; Blin, J.; Volle, G.; Motuzas, J.; Julbe, A. In Situ Generation of Ni Metal Nanoparticles as Catalyst for H2-Rich Syngas Production from Biomass Gasification. Appl. Catal. A Gen. 2010, 382, 220–230.

(18)

Huang, Y.; Yin, X.; Wu, C.; Wang, C.; Xie, J.; Zhou, Z.; Ma, L.; Li, H. Effects of Metal Catalysts on CO2 Gasification Reactivity of Biomass Char. Biotechnol. Adv. 2009, 27, 568–572.

(19)

Lahijani, P.; Zainal, Z. A.; Mohamed, A. R. Catalytic Effect of Iron Species on CO2 Gasification Reactivity of Oil Palm Shell Char. Thermochim. Acta 2012, 546,


23


Page 24 of 26

24–31. (20)

Ma, C.; Backman, R.; Öhman, M. Thermochemical Equilibrium Study of Slag Formation during Pressurized Entrained-Flow Gasification of Woody Biomass. Energ Fuel 2015, 29, 4399−4406.

(21)

Konttinen, J.; Backman, R.; Hupa, M.; Moilanen, A.; Kurkela, E. Trace Element Behavior in the Fluidized Bed Gasification of Solid Recovered Fuels – A Thermodynamic Study. Fuel 2013, 106, 621–631.

(22)

Koukkari, P.; Penttilä, K.; Hack, K.; Petersen, S. CHEMSHEET – An Efficient Worksheet Tool for Thermodynamic Process Simulation. In Microstructures, Mechanical Properties and Processes - Computer Simulation and Modelling, Volume 3; Bréchet, Y., Ed.; Wiley-VCH: Weinheim, 2000; pp 323–330.

(23)

Kangas, P.; Koukkari, P.; Hupa, M. Modeling Biomass Conversion during Char Gasification, Pyrolysis, and Torrefaction by Applying Constrained Local Thermodynamic Equilibrium. Energy Fuels 2014, 28, 6361–6370.

(24)

Yung, M. M.; Jablonski, W. S.; Magrini-Bair, K. A. Review of Catalytic Conditioning of Biomass-Derived Syngas. Energy Fuels 2009, 23 (4), 1874–1887.

(25)

Said, M.; Cassayre, L.; Dirion, J.-L.; Joulia, X.; Nzihou, A. Effect of Nickel Impregnation on Wood Gasification Mechanism. Waste and Biomass Valorization 2017, 8, 2843–2852.

(26)

Said, M.; Cassayre, L.; Dirion, J.-L.; Nzihou, A.; Joulia, X. Behavior of Heavy Metals during Gasification of Phytoextraction Plants: Thermochemical Modelling. Comput. Aided Chem. Eng. 2015, 37, 341–346.

(27)

Said, M.; Cassayre, L.; Dirion, J.-L.; Joulia, X.; Nzihou, A. On the Relevance of Thermodynamics to Predict the Behaviour of Inorganics during CO2. Comput. Aided Chem. Eng. 2017, 40, 2671–2676.

(28)

Degroot, W. F.; Shafizadeh, F. The Influence of Exchangeable Cations on the Carbonization of Biomass. J. Anal. Appl. Pyrolysis 1984, 6, 217–232.

(29)

Mahar, A.; Wang, P.; Ali, A.; Awasthi, M. K.; Lahori, A. H.; Wang, Q.; Li, R.; Zhang, Z. Challenges and Opportunities in the Phytoremediation of Heavy Metals Contaminated Soils : A Review. Ecotoxicol. Environ. Saf. 2016, 126, 111–121.

(30)

Bale, C. W.; Bélisle, E.; Chartrand, P.; Decterov, S.; Eriksson, G.; Hack, K.; Jung, I.-H.; Kang, Y.-B.; Melançon, J.; Pelton, A. D.; Robelin, C.; Peterson, S. FactSage Thermochemical Software and Databases — Recent Developments. Calphad 2009, 33, 295–311.


24

Page 25 of 26 1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60


(31)

Lindberg, D.; Backman, R.; Chartrand, P.; Hupa, M. Towards a Comprehensive Thermodynamic Database for Ash-Forming Elements in Biomass and Waste Combustion — Current Situation and Future Developments. Fuel Process. Technol. J. 2013, 105, 129–141.

(32)

Yang, H.; Yan, R.; Chen, H.; Lee, D. H.; Zheng, C. Characteristics of Hemicellulose, Cellulose and Lignin Pyrolysis. Fuel 2007, 86, 1781–1788.

(33)

Figueiredo, J. L.; Rivera-Utrilla, J.; Ferro-Garcia, M. A. Gasification of Active Carbons of Different Texture Impregnated with Nickel, Cobalt and Iron. Carbon 1987, 25, 703–708.

(34)

Duman, G.; Uddin, Md. A.; Yanik, J. The Effect of Char Properties on Gasification Reactivity. Fuel Process. Technol. 2014, 118, 75–81.

(35)

Di Blasi, C. Combustion and Gasification Rates of Lignocellulosic Chars. Prog. Energy Combust. Sci. 2009, 35, 121–140.

(36)

Jang, W.-J.; Jeong, D.-W.; Shim, J.-O.; Kim, H.-M.; Roh, H.-S.; Son, I. H.; Lee, S. J. Combined Steam and Carbon Dioxide Reforming of Methane and Side Reactions: Thermodynamic Equilibrium Analysis and Experimental Application. Appl. Energy 2016, 173, 80–91.

(37)

Butterman, H. C.; Castaldi, M. J. CO2 as a Carbon Neutral Fuel Source via Enhanced Biomass Gasification. Environ. Sci. Technol. 2009, 43, 9030–9037.

(38)

Kaknics, J.; Defoort, F.; Poirier, J. Inorganic Phase Transformation in Miscanthus Ash. Energ Fuel 2015, 29, 6433–6442.

(39)

Mortensen, P. M.; Dybkjær, I. Industrial Scale Experience on Steam Reforming of CO2-Rich Gas. Appl. Catal. A Gen. 2015, 495, 141–151.

(40)

Woolcock, P. J.; Brown, R. C. A Review of Cleaning Technologies for BiomassDerived Syngas. Biomass Bioenergy 2013, 52, 54–84.


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Influence of Nickel on Biomass Pyro-Gasification - ACS Publications

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